Biosynthetic pathways and products

ABSTRACT

This disclosure describes biosynthesized compounds including anhydromevalonolactone and β-methyl-δ-valerolactone. This disclosure further describes biosynthetic methods for making these compounds. In some embodiments, the biosynthetic methods can include a combination of biosynthesis and chemical steps to produce β-methyl-δ-valerolactone. Finally, this disclosure described recombinant cells useful for the biosynthesis of these compounds.

CROSS-REFERENCE TO RELATED APPLICATION

This application claims priority to U.S. Provisional Patent Application Ser. No. 61/813,354, filed Apr. 18, 2013 and U.S. Provisional Patent Application Ser. No. 61/866,233, filed Aug. 15, 2013, each of which is incorporated herein by reference.

SUMMARY

This disclosure describes, in one aspect, biosynthesized compounds including anhydromevalonolactone and β-methyl-δ-valerolactone. In another aspect, this disclosure further describes biosynthetic methods for making these compounds. In some embodiments, the biosynthetic methods can include a combination of biosynthesis and chemical steps to produce β-methyl-δ-valerolactone. In yet another aspect, this disclosure described recombinant cells useful for the biosynthesis of these compounds.

The above summary of the present invention is not intended to describe each disclosed embodiment or every implementation of the present invention. The description that follows more particularly exemplifies illustrative embodiments. In several places throughout the application, guidance is provided through lists of examples, which examples can be used in various combinations. In each instance, the recited list serves only as a representative group and should not be interpreted as an exclusive list.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1. Bio-based routes to β-methyl-δ-valerolactone (βMδVL). (I) Full artificial synthetic pathway. atoB: acetyl-CoA acetyltransferase; mvaS: HMG-CoA synthase; mvaE: HMG-CoA reductase; sidI: acyl-CoA ligase; sidH: enoyl-CoA hydratase; ter: enoyl-CoA reductase. (II) Hybrid pathway. Biosynthesized mevalonate is converted to βMδVL through catalytic dehydration and hydrogenation. (III) Intermediate anhydromevalonyl-CoA can spontaneously cyclize to anhydromevalonolactone.

FIG. 2. Plasmids constructed for testing βMδVL production.

FIG. 3. Total biobased production of β-methyl-δ-valerolactone and semisynthetic route to this monomer. (A) Fermentation of mevalonate from different combinations of MvaS and MvaE. I: MvaS from E. faecalis, MvaE from E. faecalis; II: MvaS from S. aureus, MvaE from E. faecalis; III: MvaS from L. casei, MvaE from E. faecalis; IV: MvaS from L. casei, MvaE from S. aureus; V: MvaS from L. casei, MvaE from L. casei; VI: MvaS from L. casei, MvaE from M. maripaludis; VII: MvaS from L. casei, MvaE from M. voltae. (B) Anhydromevalonolactone fermentation with siderophore enzymes SidI and SidH from: A, A. fumigatus; B, N. crassa; C, P. nodorum; D, S. sclerotiorum. (C) Production of β-methyl-δ-valerolactone through fermentation with enoate-reductase: 1, Oye2 from S. cerevisiae; 2, Oye3 from S. cerevisiae; 3, wild-type YqjM from B. subtilis; 4, Mutant YqjM (C26D and I69T) from B. subtilis. (D) Production of mevalonate by fermentation of glucose in a 1.3 L bioreactor.

FIG. 4. Acid catalyzed dehydration of mevalonate to anhydromevalonolactone monitored by refractive index (RI).

FIG. 5. Dehydration of mevalonate fermentation sample to anhydromevalonolactone catalyzed by sulfuric acid. (A) reaction with different sulfuric acid concentration. (B) HPLC measurement.

FIG. 6. NMR spectrum the extracted anhydromevalonolactone.

FIG. 7. NMR spectrum hydrogenated sample of anhydromevalonolactone.

FIG. 8. Alternative bio-based routes to β-methyl-δ-valerolactone (βMδVL). atoB: acetyl-CoA acetyltransferase; mvaS: HMG-CoA synthase; mvaE: HMG-CoA reductase; sidI: acyl-CoA ligase; sidH: enoyl-CoA hydratase; OYE2: enoate-reductase.

FIG. 9. Plasmids constructed for testing β-methyl-δ-valerolactone (βMδVL) production.

FIG. 10. 500 L fermentation curve.

DETAILED DESCRIPTION OF ILLUSTRATIVE EMBODIMENTS

This disclosure relates to biosynthetic pathways—and genetically modified microbes that possess those pathways—useful for the production of β-methyl-δ-valerolactone. This disclosure describes a full biosynthetic pathway to biosynthesize 3-methyl-5-hydroxypentanoyl-CoA from a renewable carbon source. As shown in FIG. 1, 3-methyl-5-hydroxypentanoyl-CoA spontaneously converts to the end product, β-methyl-δ-valerolactone. Alternatively, as shown in FIG. 8, anhydromevalonyl-CoA spontaneously cyclizes to anhydromevalonolactone, which can be reduced to β-methyl-δ-valerolactone. This disclosure also describes an integrated process to produce β-methyl-δ-valerolactone that involves conversion of either anhydromevalonyl-CoA or mevalonate to anhydromevalonolactone, then chemical processing of anhydromevalonolactone to produce β-methyl-δ-valerolactone.

Currently, polylactide (PLA) is an example of a bio-based renewable polymer that has significant market impact. However, the semi-crystalline nature of PLA has limited its applications. This disclosure describes development of an innovative fermentation processes for novel polymer monomers that can polymerize into amorphous structures.

Design and Construct a Novel Synthetic Metabolic Pathway

No naturally-existing microbial metabolic pathway produces β-methyl-δ-valerolactone directly from a carbohydrate carbon source such as, for example, glucose. We have designed and engineered non-natural metabolic pathways to β-methyl-δ-valerolactone (FIG. 1 and FIG. 8).

First, we introduced a heterologous pathway into a microbial host to produce a non-native metabolite mevalonate. (FIG. 1, Route I) The mevalonate pathway exists in mammals and Archaea for lipid biosynthesis. Since many microbes, e.g., E. coli, naturally possess a metabolic pool of acetyl-CoA, conversion of mevalonate to anhydromevalonyl-CoA can be accomplished in two enzymatic steps. We further designed and engineered a pathway that involves cloning acyl-CoA ligase (sidI) and enoyl-CoA hydratase (sidH). Finally, we engineered microbes to reduce the double bond of anhydromevalonyl-CoA to form 3-methyl-5-hydroxy-pentanoyl-CoA, catalyzed by trans-2-enoyl-CoA reductase (ter). 3-methyl-5-hydroxy-pentanoyl-CoA can spontaneously cyclize into β-methyl-δ-valerolactone.

We also have designed a hybrid approach to producing β-methyl-δ-valerolactone (FIG. 1, Route II). First, mevalonate is biosynthesized from a renewable carbon source. Then, mevalonate is converted to anhydromevalonolactone by catalytic dehydration Anhydromevalonolactone is extracted from the reaction mixture and reduced to β-methyl-δ-valerolactone through catalytic hydrogenation. We also observed that the intermediate anhydromevalonyl-CoA could spontaneously cyclize to anhydromevalonolactone (FIG. 1, Route III), thus providing another biosynthetic/chemical hybrid route to β-methyl-δ-valerolactone.

We also have designed a non-natural pathway to produce β-methyl-δ-valerolactone (FIG. 8). Here again, we introduced a heterologous pathway into a microbial host to produce a non-native metabolite mevalonate. We again exploit the activities of sidI and sidH to generate anhydromevalonyl-coA, which can spontaneously cyclize into anhydromevalonolactone. Finally, we introduced an enoate reductase (e.g., OYE2, YqjM; Bougioukou et al., 2009, Advanced Synthesis & Catalysis 351:3287-3305) to reduce the double bond of anhydromevalonolactone to form β-methyl-δ-valerolactone.

Optimization of Mevalonate Production in Shake Flask

Mevalonate is the immediate metabolic precursor for our artificial biosynthetic pathway. While there was previous attempt to produce this compound in E. coli, the production yield and level was impractically low for industrial production. Here, we report the recombinant production of mevalonate. Specifically, we explored the effect of different combinations of HMG-CoA synthase (MvaS) and HMG-CoA reductase (MvaE). The mevalonate titer was increased 14% when using mvaS from L. casei instead of that from E. faecalis in shake flask (FIG. 3A). The strain carrying mvaS from L. casei was further optimized by substituting different mvaE genes. The strain with both mvaS and mvaE from L. casei produced 14.6 g/L mevalonate, which was 36% higher than the original strain with mvaS of L. casei and mvaE of E. faecalis (FIG. 3A). The combination with mvaS and mvaE from L. casei produced 50% more mevalonate than a previously reported construct with possessing mvaS and mvaE from E. faecalis. (Tabata et al. 2004, Biotechnol Lett 26:1487-1491).

Mevalonate Production in 1.3 L Bioreactor

The strain carrying mvaS and mvaE from L. casei was chosen to perform scale-up fermentation in a 1.3 L bioreactor. The biomass increased to 38 g/L after 24 hours, and then decreased gradually during fermentation (FIG. 3D). Acetate accumulated to 2.3 g/L in the first six hours due to fast growth rate, then decreased and maintained at a very low level until 32 hours. As the concentration of mevalonate reached 51 g/L, the glucose consumption rate decreased and acetate increased gradually. When acetate reached 3.5 g/L after 48 hours, fermentation was stopped. The mevalonate productivity was around 2 gL⁻¹h⁻¹ throughout the whole fermentation process. The final titer of mevalonate after 48 hours was 88.3 g/L, and the yield from glucose is around 0.26 g/g. The mevalonate titer was increase 87.9% compared to the previous report. (Tabata et al. 2004, Biotechnol Lett 26:1487-1491).

After introducing the second plasmid pZAlac-sidI-sidH-ter into the mevalonate-producing E. coli, we detected about 20 mg/L anhydromevalonolactone, but β-methyl-δ-valerolactone or its hydrolyzed acid form was not found in the fermentation broth.

Catalytic Dehydration and Extraction

Though anhydromevalonolactone can be converted into β-methyl-δ-valerolactone by catalytic hydrogenation, its fermentation concentration was still too low for industrial application. Thus, we developed an alternative approach by chemically converting mevalonate into β-methyl-δ-valerolactone (Route II, FIG. 1). Sulfuric acid was chosen as the catalyst to enable dehydration reaction. 5 mL fermentation samples with an addition of 0.1 to 0.6 mL sulfuric acid were placed in 15 mL test tubes. The reaction was performed in an autoclave for one hour (121° C., 15 psi). Almost all the mevalonate was converted into anhydromevalonolactone when 5 mL H₂SO₄ was used (FIGS. 5A and 5B), which suggested that acid was a selective catalyst to dehydrate the tertiary alcohol group.

Purification of anhydromevalonolactone also was studied by extraction with different organic solvents (Table 1). Approximately 96% of the anhydromevalonolactone was extracted when chloroform was applied at a 1:1 volume ratio. The partition coefficient Kd for anhydromevalonolactone in between chloroform and water was 25. NMR analysis indicated the anhydromevalonolactone was in the lactone form, instead of equilibrating with its hydroxyacid form (FIG. 6).

TABLE 1 The extract efficiency and Kd of different solvents Anhydromevalonolactone Solvents extract efficiency (%) Kd MIBK 79.90 3.97 DIBK 44.15 0.79 Oley 35.56 0.55 ethyl acetate 79.67 3.92 CHCl3 96.14 24.89 Benzene 65.26 1.88

Hydrogenation

Anhydromevalonolactone (5.7 g) was dissolved in 700 mL methanol. Catalyst Pd/C (2 g) was added. The pressure of H₂ was maintained at 4 bar. After reaction at 25° C. overnight (˜14 hours), the product was column purified and the oily β-methyl-δ-valerolactone was obtained with a yield of 87.93% (FIG. 7).

Alternative Biosynthesis of Anhydromevalonolactone and Mevalonolactone

Alternative pathways to producing anhydromevalonolactone involve further modifying a microbe to include sidI and sidH from Aspergillus fumigatus, Neurospora crassa, Phaeosphaeria nodorum, or Sclerotinia sclerotiorum. Table 2 shows anhydromevalonolactone fermentation results when the sidI-sidH-containing plasmids were introduced into mevalonate-producing E. coli. The strain carrying sidI and sidH from Aspergillus fumigatus produced 730 mg/L anhydromevalonolactone; the strain carrying sidI and sidH from Neurospora crassa produced 540 mg/L anhydromevalonolactone.

TABLE 2 The anhydromevalonolactone fermentation results (g/L) Anhydro- Strain Mevalonate mevalonolactone BW25113 with pMEV-7 and pAML-1 12.36 ± 1.18 0.73 ± 0.06 BW25113 with pMEV-7 and pAML-2 13.59 ± 0.24 0.54 ± 0.02

Enoate reductases such as, for example, OYE2 and OYE3 from S. cerevisiae or ygjM from B. subtilis can catalyze reactions using 3-methylcyclohexenone and/or 3-methylcyclohexanone as a native substrate. We introduced coding regions for OYE2, OYE3, wild type ygjM, or a mutant ygjM into an anhydromevalonolactone-producing microbe to determine whether each construct could synthesize the final monomer of mevalonolactone. Results are shown in Table 3.

TABLE 3 The βMδVL fermentation results (g/L) Anhydrome- Strain Mevalonate valonolactone βMδVL BW25113 with pMEV-7 10.19 ± 0.61  0.34 ± 0.03 0.18 ± 0.03 and pMVL-1 BW25113 with pMEV-7 6.77 ± 0.58 0.48 ± 0.03 0 and pMVL-2 BW25113 with pMEV-7 8.85 ± 0.56 0.55 ± 0.01 0 and pMVL-3 BW25113 with pMEV-7 9.39 ± 0.48 0.31 ± 0.01 0.27 ± 0.02 and pMVL-4

Thus, in one aspect, this disclosure describes biosynthesized compounds, recombinant microbes that produce the biosynthesized compounds, and methods of producing the biosynthesized compounds. As used herein, a “biosynthesized compound” is a compound in which at least one step of its synthesis is performed by a microbe. In some cases, the biosynthesized compound may be β-methyl-δ-valerolactone. As illustrated in FIG. 1 and FIG. 8, there are multiple routes by which a biosynthesized β-methyl-δ-valerolactone compound may be produced. Route I involves biosynthesis of β-methyl-δ-valerolactone by a microbe from a carbon source in a culture medium. Route II and Route III illustrated in FIG. 1 show that an intermediate compound (e.g., biosynthesized anhydromevalonolactone) may be harvested and subjected to one or more chemical steps to produce biosynthesized β-methyl-δ-valerolactone. The pathway illustrated in FIG. 8 involves an alternative fully biosynthetic route to β-methyl-δ-valerolactone.

One can distinguish a biosynthesized compound as described herein from a similar compound produced by conventional chemical processes from, for example, a petroleum-based material by the ratio of ¹⁴C to ¹²C in a sample of the compound. A sample of the compound that is biosynthesized will possess a measurable amount of ¹⁴C isotopes incorporated into the compound molecules, while a sample of the compound prepared from petroleum-based materials will possess negligible levels of ¹⁴C. Thus, a sample or composition that includes a biosynthesized compound (e.g., either β-methyl-δ-valerolactone or anhydromevalonolactone) will possess a ¹⁴C/¹²C ratio greater than zero. In some cases, a sample or composition that includes a biosynthesized compound can have a ¹⁴C/¹²C ratio greater than 0.25×10¹² such as, for example, a ¹⁴C/¹²C ratio from 0.25×10¹² to 1.2×10¹².

A biosynthesized compound as described herein, whether β-methyl-δ-valerolactone and/or anhydromevalonolactone, is produced by a method, described in more detail below, in which a host cell is modified to be a recombinant cell that can exhibit increase biosynthesis of the biosynthetic compound compared to a wild-type control. In some cases, the wild-type control may be unable to produce the biosynthetic compound and, therefore, an increase in the biosynthesis of the biosynthetic compound may reflect any measurable biosynthesis of that compound. In certain embodiments, an increase in the biosynthesis of a biosynthetic compound can include biosynthesis sufficient for a culture of the microbial cell to accumulate the biosynthetic compound to a predetermine concentration.

The predetermined concentration may be any predetermined concentration of the biosynthetic compound suitable for a given application. Thus, a predetermined concentration may be, for example, a concentration of at least 0.1 g/L such as, for example, at least 0.25 g/L, at least 0.5 g/L, at least 1.0 g/L, at least 2.0 g/L, at least 3.0 g/L, at least 4.0 g/L, at least 5.0 g/L, at least 6.0 g/L, at least 7.0 g/L, at least 8.0 g/L, at least 9.0 g/L, at least 10 g/L, at least 20 g/L, at least 50 g/L, at least 100 g/L, or at least 200 g/L.

Thus, in another aspect, this disclosure describes methods of making biosynthesized compounds including, for example, β-methyl-δ-valerolactone and/or anhydromevalonolactone. FIG. 1 illustrates three different exemplary biosynthetic routes to producing β-methyl-δ-valerolactone. FIG. 8 illustrates an alternative exemplary biosynthetic routes to producing β-methyl-δ-valerolactone.

One method, illustrated as Route I in FIG. 1, involves biosynthesis by a recombinant cell of 3-methyl-5-hydroxypentanoyl-CoA, which spontaneously converts to β-methyl-δ-valerolactone. Thus, in some embodiments, the method includes culturing an appropriate recombinant cell—described in more detail below—under conditions effective for the recombinant cell to exhibit increased biosynthesis of 3-methyl-5-hydroxypentanoyl-CoA compared to a wild-type control, then allowing the 3-methyl-5-hydroxypentanoyl-CoA to spontaneously convert to β-methyl-δ-valerolactone.

In alternative embodiments, the methods can include a combined biosynthetic-chemical approach. In some of these embodiments, reflected in Route III in FIG. 1, a recombinant cell modified to exhibit increased biosynthesis of anhydromevalonyl-CoA compared to a wild-type control can be grown in culture under conditions effective for the recombinant cell to produce anhydromevalonyl-CoA. The anhydromevalonyl-CoA may be harvested and allowed to spontaneously convert to anhydromevalonolactone. The anhydromevalonolactone may be converted to β-methyl-δ-valerolactone via one or more chemical steps described in more detail below.

In another combined biosynthetic-chemical approach, reflected as Route II in FIG. 1, a recombinant cell modified to exhibit increased biosynthesis of mevalonate (or its lactone form mevalonolactone) compared to a wild-type control can be grown in culture under conditions effective for the recombinant cell to produce mevalonate (or mevalonolactone). The mevalonate (or mevalonolactone) may be harvested and converted to anhydromevalonolactone. The anhydromevalonolactone may be converted to β-methyl-δ-valerolactone via one or more chemical steps described in more detail below.

In still other embodiments, the method can involve biosynthesis of anhydromevalonyl-CoA, which can spontaneously convert to anhydromevalonolactone, which can, in turn, be enzymatically converted to β-methyl-δ-valerolactone. Thus, in some embodiments, the method includes culturing an appropriate recombinant cell—described in more detail below—under conditions effective for the recombinant cell to exhibit increased biosynthesis of anhydromevalonyl-CoA and increased conversion of anhydromevalonolactone to β-methyl-δ-valerolactone.

In some embodiments, the conversion of mevalonate (or mevalonolactone) to anhydromevalonolactone can include dehydrating the mevalonate (or mevalonolactone) using a dehydration catalyst under appropriate conditions for the dehydration catalyst to dehydrate the mevalonate (or mevalonolactone) to anhydromevalonolactone. Exemplary dehydration catalysts can include, for example, tosylic acid, sulfuric acid and phosphoric acid, or solid acid catalysts such as zeolites, Amberlyst 70 and Amberlyst 15. In some embodiments, the dehydration catalyst may be provided in a catalytic amount of at least 0.1 equivalents relative to mevalonate (or mevalonolactone). In some of these embodiments, the dehydration catalyst may be provided in a catalytic amount of no more than 20.0 equivalents relative to mevalonate (or mevalonolactone). In some embodiments, the dehydration may be performed at a temperature of no less than room temperature such as for example, at least 20° C., at least 30° C., at least 40° C., at least 50° C., at least 60° C., at least 70° C., at least 80° C., at least 90° C., or at least 100° C.

The recombinant cell modified to exhibit increased biosynthesis of mevalonate (or its lactone form mevalonolactone) compared to a wild-type control can be any suitable recombinant cell. While exemplary embodiments described herein include a genetically modified E. coli host cell, the recombinant cells described herein can be constructed, and the methods of making and using the recombinant cells can be performed, using any suitable host cell. Thus, the recombinant cell can be, or be derived from, any suitable microbe including, for example, a prokaryotic microbe or a eukaryotic microbe. As used herein, the term “or derived from” in connection with a microbe simply allows for the “host cell” to possess one or more genetic modifications before being modified to exhibit the indicated increased biosynthetic activity. Thus, the term “recombinant cell” encompasses a “host cell” that may contain nucleic acid material from more than one species before being modified to exhibit the indicated biosynthetic activity.

In some embodiments, the host cell may be selected to possess one or more natural physiological activities. For example, the host cell may be photosynthetic (e.g., cyanobacteria) or may be cellulolytic (e.g., Clostridium cellulolyticum).

In some embodiments, the recombinant cell may be, or be derived from, a eukaryotic microbe such as, for example, a fungal cell. In some of these embodiments, the fungal cell may be, or be derived from, a member of the Saccharomycetaceae family such as, for example, Saccharomyces cerevisiae, Candida rugosa, or Candida albicans. In some of these embodiments, yield can be improved by at least partially knocking out activity of the host cell's native mevalonate consuming pathways.

In other embodiments, the recombinant cell may be, or be derived from, a prokaryotic microbe such as, for example, a bacterium. In some of these embodiments, the bacterium may be a member of the phylum Protobacteria. Exemplary members of the phylum Protobacteria include, for example, members of the Enterobacteriaceae family (e.g., Escherichia coli) and, for example, members of the Pseudomonaceae family (e.g., Pseudomonas putida). In other cases, the bacterium may be a member of the phylum Firmicutes. Exemplary members of the phylum Firmicutes include, for example, members of the Bacillaceae family (e.g., Bacillus subtilis), members of the Clostridiaceae family (e.g., Clostridium cellulolyticum) and, for example, members of the Streptococcaceae family (e.g., Lactococcus lactis). In other cases, the bacterium may be a member of the phylum Cyanobacteria. Here again, in some of these embodiments, yield can be improved by at least partially knocking out activity of the host cell's native mevalonate consuming pathways.

In some embodiments, the recombinant cell can exhibit increased activity compared to a wild-type control of one or more enzymes involved in a metabolic biosynthetic pathway for producing mevalonate (or mevalonolactone). As used herein, the terms “activity” with regard to particular enzyme refers to the ability of a polypeptide, regardless of its common name or native function, to catalyze the conversion of the enzyme's substrate to a product, regardless of whether the “activity” as less than, equal to, or greater than the native activity of the identified enzyme. Methods for measuring the biosynthetic activities of cells are routine and well known to those of ordinary skill in the art.

As used herein, an increase in catalytic activity can be quantitatively measured and described as a percentage of the catalytic activity of an appropriate wild-type control. The catalytic activity exhibited by a genetically-modified polypeptide can be, for example, at least 110%, at least 125%, at least 150%, at least 175%, at least 200% (two-fold), at least 250%, at least 300% (three-fold), at least 400% (four-fold), at least 500% (five-fold), at least 600% (six-fold), at least 700% (seven-fold), at least 800% (eight-fold), at least 900% (nine-fold), at least 1000% (10-fold), at least 2000% (20-fold), at least 3000% (30-fold), at least 4000% (40-fold), at least 5000% (50-fold), at least 6000% (60-fold), at least 7000% (70-fold), at least 8000% (80-fold), at least 9000% (90-fold), at least 10,000% (100-fold), or at least 100,000% (1000-fold) of the activity of an appropriate wild-type control.

Alternatively, an increase in catalytic activity may be expressed as at an increase in k_(cat) such as, for example, at least a two-fold increase, at least a three-fold increase, at least a four-fold increase, at least a five-fold increase, at least a six-fold increase, at least a seven-fold increase, at least an eight-fold increase, at least a nine-fold increase, at least a 10-fold increase, at least a 15-fold increase, or at least a 20-fold increase in the k_(cat) value of the enzymatic conversion.

An increase in catalytic activity also may be expressed in terms of a decrease in K_(m) such as, for example, at least a two-fold decrease, at least a three-fold decrease, at least a four-fold decrease, at least a five-fold decrease, at least a six-fold decrease, at least a seven-fold decrease, at least an eight-fold decrease, at least a nine-fold decrease, at least a 10-fold decrease, at least a 15-fold decrease, or at least a 20-fold decrease in the K_(m) value of the enzymatic conversion.

A decrease in catalytic activity can be quantitatively measured and described as a percentage of the catalytic activity of an appropriate wild-type control. The catalytic activity exhibited by a genetically-modified polypeptide can be, for example, no more than 95%, no more than 90%, no more than 85%, no more than 80%, no more than 75%, no more than 70%, no more than 65%, no more than 60%, no more than 55%, no more than 50%, no more than 45%, no more than 40%, no more than 35%, no more than 30%, no more than 25%, no more than 20%, no more than 15%, no more than 10%, no more than 5%, no more than 4%, no more than 3%, no more than 2%, no more than 1% of the activity, or 0% of the activity of a suitable wild-type control.

Alternatively, a decrease in catalytic activity can be expressed as an appropriate change in a catalytic constant. For example, a decrease in catalytic activity may be expressed as at a decrease in k_(cat) such as, for example, at least a two-fold decrease, at least a three-fold decrease, at least a four-fold decrease, at least a five-fold decrease, at least a six-fold decrease, at least a seven-fold decrease, at least an eight-fold decrease, at least a nine-fold decrease, at least a 10-fold decrease, at least a 15-fold decrease, or at least a 20-fold decrease in the k_(cat) value of the enzymatic conversion.

A decrease in catalytic activity also may be expressed in terms of an increase in K_(m) such as, for example, an increase in K_(m) of at least two-fold, at least three-fold, at least four-fold, at least five-fold, at least six-fold, at least seven-fold, at least an eight-fold, at least nine-fold, at least 10-fold, at least 15-fold, at least 20-fold, at least 25-fold, at least 30-fold, at least 35-fold, at least 40-fold, at least 45-fold, at least 50-fold, at least 75-fold, at least 100-fold, at least 150-fold, at least 200-fold, at least 230-fold, at least 250-fold, at least 300-fold, at least 350-fold, or at least 400-fold.

Exemplary enzymes that may be part of such an engineered biosynthetic pathway include, for example, a thiolase, 3-hydroxy-3-methyl-glutaryl (HMG)-CoA synthase, and HMG-CoA reductase. The thiolase may be any suitable thiolase that is natively expressed by any organism. In some embodiments, the thiolase can include AtoB such as, for example, the enzyme encoded by a polynucleotide that includes the atoB coding region isolated from E. coli. The HMG-CoA synthase may be any suitable HMG-CoA synthase that is natively expressed by any organism. In some embodiments, the HMG-CoA synthase can include MvaS such as, for example, an enzyme encoded by a polynucletide that includes a myaS coding region isolated from a member of the genus Enterococcus, a member of the genus Staphylococcus, a member of the genus Lactobacillus, or a member of the genus Methanococcus. The HMG-CoA reductase may be any suitable HMG-CoA reductase that is natively expressed by any organism. In some embodiments, the HMG-CoA reductase can include MvaE such as, for example, an enzyme encoded by a polynucleotide that includes a myaE coding region isolated from a member of the genus Enterococcus, a member of the genus Staphylococcus, a member of the genus Lactobacillus, or a member of the genus Methanococcus.

In some embodiments, the method may be performed by growing the recombinant cells in a cell culture that includes medium that has, as a carbon source, one or more of glucose, glycerol, xylose, arabinose, glucaric acid, galactaric acid, galacturonic acid, alginate, starch, sucrose, or cellulose.

Regardless of whether one follows Route II, Route III, or some other metabolic route to anhydromevalonolactone, the anhydromevalonolactone may be converted to β-methyl-δ-valerolactone by catalytic hydrogenation of the anhydromevalonolactone. In some embodiments, the anhydromevalonolactone may be hydrogenated in an organic solvent in the presence of a heterogeneous catalyst or homogenous catalyst. Exemplary heterogeneous catalysts include, for example, palladium on activated carbon, nickel on silica, and nickel on alumina. Exemplary homogenous catalysts include, for example, NaBH₄, LiAlH₄, sulfuric acid, phosphoric acid, and mevalonic acid. The catalytic hydrogenation of anhydromevalonolactone may be performed under any appropriate set of conditions. For example, the catalytic hydrogenation of anhydromevalonolactone may be performed at a temperature of no more than 100° C. and/or at a hydrogen pressure of no more than 100 bar.

β-methyl-δ-valerolactone so produced may be collected by any suitable method including, for example, distilling the β-methyl-δ-valerolactone such as, for example, by using a staged distillation column at a pressure of no more than 1 atm.

In some embodiments, one can obtain β-methyl-δ-valerolactone with a recovery rate of at least 70% such as, for example, at least 75%, at least 80%, at least 85%, or at least 90%.

In some embodiments, the method can include a step of extracting the anhydromevalonolactone prior to the catalytic dehydrogenation. Such a step can increase the efficiency of the catalytic dehydrogenation of anhydromevalonolactone and, therefore, increase the final yield of β-methyl-δ-valerolactone. In some embodiments, the extraction may be performed using a water-immiscible extractant such as, for example, an amide, an ether, a ketone, an alkane, an alcohol, an ester, benzene, xylene, chloroform, or any combination of two or more water-immiscible extractants. In some of these embodiments, the extraction can recover at least 70% of the anhydromevalonolactone such as, for example, at least 75%, at least 80%, at least 85%, or at least 90% of the anhydromevalonolactone. Even with a recovery of less than 100% of the anhydromevalonolactone, the increased concentration of anhydromevalonolactone that results from an extraction step can improve the ultimate yield of β-methyl-δ-valerolactone.

In some embodiments, anhydromevalonolactone may be biosynthetically converted to O-methyl-δ-valerolactone. Exemplary enzymes that may catalyze the biosynthetic conversion of anhydromevalonolactone to β-methyl-δ-valerolactone includes, for example, an enoate reductase. In some embodiments, the enoate reductase can include, for example, OYE2 or OYE3 such as, for example, an enzyme encoded by a polynucleotide that includes an oye2 or oye3 coding region isolated from a member of the Saccharomycetaceae family such as, for example, Saccharomyces cerevisiae. In other embodiments, the enoate reductase can include, for example, YqjM such as, for example, an enzyme encoded by a polynucleotide a ygjM coding region isolated from a member of the Bacillaceae family such as, for example, Bacillus subtilis.

A recombinant cell useful for biosynthesis of mevalonate is described above. As described above, such a recombinant cell may be used to produce a biosynthetic compound as described herein—e.g., anhydromevalonolactone and/or β-methyl-δ-valerolactone—via Route II illustrated in FIG. 1. Alternatively, a recombinant cell useful for biosynthesis of mevalonate (or mevalonolactone) may be further modified to biosynthesize anhydromevalonolactone (anhydromevalonate) and/or β-methyl-δ-valerolactone via Route I or Route III illustrated in FIG. 1. Thus, in another aspect, this disclosure describes recombinant cells useful for biosynthesis according to Route I or Route III as illustrated in FIG. 1.

In some embodiments, the recombinant cell can be modified to exhibit increased biosynthesis of anhydromevalonyl-CoA compared to a wild-type control. Such a recombinant cell can exhibit increased activity, compared to a wild-type control, of a thiolase, a HMG-CoA synthase, and/or a HMG-CoA reductase, as described above with respect to recombinant cells useful for biosynthesis of mevalonate (or mevalonolactone). In addition, a recombinant cell useful for biosynthesis of anhydromevalonyl-CoA and/or anhydromevalonolactone (or anhydromevalonate) can be modified to exhibit increased activity compared to a wild-type control of an acyl-CoA ligase and/or an enoyl-CoA hydratase.

The acyl-CoA ligase may be any suitable acyl-CoA ligase that is natively expressed by any organism. In some embodiments, the acyl-CoA ligase can include SidI such as, for example, the enzyme encoded by a polynucleotide that includes the sidI coding region isolated from a microorganism that produces a siderophore that comprises an anhydromevalonyl unit. Thus, suitable exemplary acyl-CoA ligases can include an acyl-CoA ligase encoded by the coding region of a polynucleotide isolated from a member of the genus Aspergillus such as, for example, Aspergillus fumigatus. Similarly, the enoyl-CoA hydratase may be any suitable enoyl-CoA hydratase that is natively expressed by any organism. In some embodiments, the enoyl-CoA hydratase can include SidH such as, for example, the enzyme encoded by a polynucleotide that includes the sidH coding region isolated from a microorganism that produces a siderophore that comprises an anhydromevalonyl unit. Thus, suitable exemplary enoyl-CoA hydratases can include an enoyl-CoA hydratase encoded by the coding region of a polynucleotide isolated from a member of the genus Aspergillus such as, for example, Aspergillus fumigatus.

In some embodiments, the recombinant cell may be still further modified to exhibit increased biosynthesis of 3-methyl-5-hydroxypentanoyl-CoA compared to a wild-type control. In some embodiments, such a recombinant cell can exhibit an increased ability to accumulate β-methyl-δ-valerolactone in culture compared to a wild-type control. In such embodiments, the recombinant cell can be modified to exhibits increased activity, compared to a wild-type control, of a thiolase, a HMG)-CoA synthase, a HMG-CoA reductase, an acyl-CoA ligase, and/or an enoyl-CoA hydratase as described above. In addition, a recombinant cell useful for biosynthesis of 3-methyl-5-hydroxypentanoyl-CoA—which spontaneously converts to β-methyl-δ-valerolactone—can be modified to exhibit increased activity compared to a wild-type control of an enoyl-Coa reductase activity. The enoyl-CoA reductase may be any suitable enoyl-CoA that is natively expressed by any organism. In some embodiments, the enoyl-CoA reductase can include Ter such as, for example, the enzyme encoded by a polynucleotide that includes the ter coding region isolated from T. denticola.

In constructing the various recombinant cells described herein, a heterologous polynucleotide encoding a heterologous polypeptide may be inserted into a vector. As used herein, a vector is a replicating polynucleotide such as, for example, a plasmid, phage, or cosmid, to which another polynucleotide may be inserted so as to bring about the replication of the inserted polynucleotide. Construction of vectors containing a polynucleotide of the invention employs standard ligation techniques known in the art. See, e.g., Sambrook et al, Molecular Cloning: A Laboratory Manual., Cold Spring Harbor Laboratory Press (1989). A vector can permit, for example, further cloning—i.e., a cloning vector—or expression of the polypeptide encoded by the coding region—i.e., an expression vector. The term vector includes, but is not limited to, plasmid vectors, viral vectors, cosmid vectors, or artificial chromosome vectors. In one embodiment, the vector is a plasmid. Selection of a vector can depend upon a variety of desired characteristics in the resulting construct, such as a selection marker, vector replication rate, and the like.

An expression vector optionally includes regulatory sequences operably linked to the coding region. The polynucleotides described herein are not limited by the use of any particular promoter, and a wide variety of promoters are known. Promoters act as regulatory signals that bind RNA polymerase in a cell to initiate transcription of a downstream (3′ direction) coding region. The promoter used can be a constitutive or an inducible promoter. It can be, but need not be, heterologous with respect to the host cell. Exemplary promoters include, for example, trp, tac, and T7.

“Coding sequence” or “coding region” refers to a nucleotide sequence that encodes a polypeptide and, when placed under the control of appropriate regulatory sequences, expresses the encoded polypeptide. The boundaries of a coding region are generally determined by a translation start codon at its 5′ end and a translation stop codon at its 3′ end. As used herein, the term “polypeptide” refers broadly to a polymer of two or more amino acids joined together by peptide bonds. The term “polypeptide” also includes molecules that contain more than one polypeptide joined by disulfide bonds, ionic bonds, or hydrophobic interactions, or complexes of polypeptides that are joined together, covalently or noncovalently, as multimers (e.g., dimers, tetramers). Thus, the terms peptide, oligopeptide, and protein are all included within the definition of polypeptide and these terms are used interchangeably. The term “polypeptide” does not connote a specific length of a polymer of amino acids, nor does it imply or distinguish whether the polypeptide is produced using recombinant techniques, chemical or enzymatic synthesis, or is naturally occurring.

“Regulatory sequence” refers to a nucleotide sequence that regulates expression of a coding region to which it is operably linked. Nonlimiting examples of regulatory sequences include, for example, promoters, transcription initiation sites, translation start sites, translation stop sites, and terminators. “Operably linked” refers to a juxtaposition wherein the components are in a relationship permitting them to function in their intended manner. A regulatory sequence is “operably linked” to a coding region when it is joined in such a way that expression of the coding region is achieved under conditions compatible with the regulatory sequence.

The term “and/or” means one or all of the listed elements or a combination of any two or more of the listed elements; the terms “comprises” and variations thereof do not have a limiting meaning where these terms appear in the description and claims; unless otherwise specified, “a,” “an,” “the,” and “at least one” are used interchangeably and mean one or more than one; and the recitations of numerical ranges by endpoints include all numbers subsumed within that range (e.g., 1 to 5 includes 1, 1.5, 2, 2.75, 3, 3.80, 4, 5, etc.).

In the preceding description, particular embodiments may be described in isolation for clarity. Unless otherwise expressly specified that the features of a particular embodiment are incompatible with the features of another embodiment, certain embodiments can include a combination of compatible features described herein in connection with one or more embodiments.

For any method disclosed herein that includes discrete steps, the steps may be conducted in any feasible order. And, as appropriate, any combination of two or more steps may be conducted simultaneously.

The present invention is illustrated by the following examples. It is to be understood that the particular examples, materials, amounts, and procedures are to be interpreted broadly in accordance with the scope and spirit of the invention as set forth herein.

EXAMPLES Example 1 Bacterial and Growth Conditions

BW25113 (rrnB_(T14) ΔlacZ_(WJ16) hsdR514 ΔaraBAD_(AH33) ΔrhaBAD_(LD78)) was used to produce (R)-mevalonate and βMδVL. (Datsenko et al., 2000, Proc Natl Acad Sci USA 97:6640-6645) All cloning procedures were carried out in the E. coli strain XL10-gold (Stratagene, Agilent Technologies, Inc., Santa Clara, Calif.). These E. coli strains were grown in test tubes at 37° C. in 2×YT rich medium (16 g/L Bacto-tryptone, 10 g/L yeast extract and 5 g/L NaCl) supplemented with appropriate antibiotics (ampicillin 100 μg/mL and kanamycin 50 μg/mL) unless otherwise specified.

Plasmid Construction

Multiple plasmids have been constructed for the biosynthesis of βMδVL (FIG. 2 and FIG. 9). Plasmid pZElac-atoB-mvaE-mvaS is responsible for mevalonate production. Plasmid pZAlac-sidI-sidH-ter is responsible for converting mevalonate into β-methyl-δ-valerolactone. Plasmid pZAlac-sidI-sidH is responsible for converting mevalonate to anhydromevalonolactone. Plasmid pZAlac-sidI-sidH-OYE2, and variants thereof, are responsible for converting anhydromevalonolactone to β-methyl-δ-valerolactone

Primers for plasmid construction are listed in Table 4.

TABLE 4 Primers used SEQ Primer name Sequence ID NO: atoBAcc-F GGGCCC ggtacc atgAAAAATTGTGTCATCGTCAGTGC  1 atoBPst-R GGGCCC ctgcag ttaATTCAACCGTTCAATCACCATCG  2 mvaSPst-F GGGCCC ctgcag AGGAGAAATTAACT atgacaattgggattgataaaattag  3 mvaSBam-R GGGCCC ggatcc ttagtttcgataagaacgaacggtat  4 mvaEBam-F GGGCCC ggatcc AGGAGAAATTAACT atgaaaacagtagttattattgatgc  5 mvaEXba-R GGGCCC tctaga ttattgttttcttaaatcatttaaaa  6 VecAcc-R GGGCCC ggtacc tttctcctctttaatgaattcggtcagt  7 VecXba-F GGGCCC tctaga ggcatcaaataaaacgaaaggctcagtc  8 SA.mvaSPst-F GGGCCC ctgcag AGGAGAAATTAACTatgacaataggtatcgacaaaataaa  9 SA.mvaSBam-R GGGCCC ggatcc ttactctggtctgtgatattcgcgaa 10 LC.mvaSPst-F GGGCCC ctgcag AGGAGAAATTAACTatgaaaatcgggattgatgcaatcgc 11 LC.mvaSBam-R GGGCCC ggatcc ttaccgctgctgatattgacgttctt 12 Bt.mvaSPst-F GGGCCC ctgcag AGGAGAAATTAACTatgccggtcggtattgaggccatgaa 13 Bt.mvaSBam-R GGGCCC ggatcc tTatgaccagacgtactcgcggtgga 14 Mm.mvaSPst-F GGGCCC ctgcag AGGAGAAATTAACTatgaaagaagtaggtattgtaggata 15 Mm.remPst-R ttagcaccgatgatgtatgcagcaccacc Agcagcagcagtgtattcaagagcatctcc 16 Mm.remPst-F ggagatgctcttgaatacactgctgctgc Tggtggtgctgcatacatcatcggtgctaa 17 Mm.mvaSBam-R GGGCCC ggatcc ttacattctaatttttcctctgtatttc 18 Mv.mvaSPst-F GGGCCC ctgcag AGGAGAAATTAACT atgaacgaagtgggtatcgtaggata 19 Mv.remPst-R cctacaagtcccatacacatttgtatacc Agcagtacctgctttacaagcaaattctaa 20 Mv.remPst-F ttagaatttgcttgtaaagcaggtactgc Tggtatacaaatgtgtatgggacttgtagg 21 Mv.mvaSBam-R GGGCCC ggatcc ttacattctaattttttctctgtatt 22 Sa.mvaEBam-F GGGCCC ggatcc AGGAGAAATTAACT atgcaaagtttagataagaatttccg 23 Sa.mvaEXba-R GGGCCC tctaga ttattgttgtctaatttcttgtaaaa 24 Lc.mvaEBam-F GGGCCC ggatcc AGGAGAAATTAACT atgaaattttacgagttgtctccaga 25 Lc.mvaEXba-R GGGCCC tctaga tTaatcccgattttcatcttttgatt 26 Mm.mvaEBam-F GGGCCC ggatcc AGGAGAAATTAACT atggaaaataacgttaatattgaaga 27 Mm.mvaEXba-R GGGCCC tctaga ttatcttccaagttcagaatgcgctt 28 Mv.mvaEBam-F GGGCCC ggatcc AGGAGAAATTAACT atgaacaatataaaaaataataatga 29 Mv.mvaEXba-R GGGCCC tctaga ttaccttcctaattccgaatgtgctt 30 pf.sidIAcc-F GGGCCC ggtacc atggaacactcgggtttccagccgga 31 pf.sidIHind-R GGGCCC AAGCTT tTaccccttgttcatgcgctcacgca 32 bs.sidIACC-F GGGCCC ggtacc atggctgaactcatccattccacaat 33 bs.sidIHind-R GGGCCC AAGCTT tTattgacttgatgataagttgaacatt 34 re.sidIACC-F GGGCCC ggtacc atgacgatgcaggccgagtcctctcc 35 re.sidHind-R GGGCCC AAGCTT tTaggccgtcctggattcgctgagtt 36 ec.sidIAcc-F GGGCCC ggtacc atgGATATCATTGGCGGACAACATCT 37 ec.sidIHind-R GGGCCC AAGCTT ttaTTTCAGATTCTTTCTAATTATTT 38 mm.sidIAcc-F GGGCCC ggtacc atgctttttacaaacgatacccttgg 39 mm.sidIAccrem-R tggctgtactctgcaataaacatggttggCaccccataaagggcagtacacttttcttt 40 mm.sidIAccrem-F aaagaaaagtgtactgccctttatggggtGccaaccatgtttattgcagagtacagcca 41 mm.sidIHind-R GGGCCC AAGCTT ttataattcttccgtttcttttttca 42 terNheI-F GGGCCCgctagcAGGAGAAATTAACTATGATTATCAAACCGATGATTCGCAG 43 terBam-R GGGCCCggatccTTAAACAACGTCCATGCGCTCGACAT 44 SidHind-F GGGCCCaagcttAGGAGAAATTAACTATGAGCACCGAGGCTCATCCTACTGT 45 SidHsal-R GGGCCCgtcgacTTACAACTTGCTCGGGCGCCATTGCG 46 OYE2sal-F GGGCCCgtcgacAGGAGAAATTAACTATGCCATTTGTTAAGGACTTTAAGCC 47 OYE2-Vec gagcctttcgttttatttgatgcctctagaGCTAGCTTAATTTTTGTCCCAACCGAGTTT 48 OYE3sal-F GGGCCCgtcgacAGGAGAAATTAACTATGCCATTTGTAAAAGGTTTTGAGCC 49 OYE3-Vec gagcctttcgttttatttgatgcctctagaGCTAGCTtAGTTCTTGTTCCAACCTAAATC 50 yqjM-F GGGCCCgtcgacAGGAGAAATTAACTatgGCCAGAAAATTATTTACACCTAT 51 yqjM-Vec gagcctttcgttttatttgatgcctctagaGCTAGCttaCCAGCCTCTTTCGTATTGAAC 52 yqjMC26D-R TTCCGTCCTTTTCATGAGAAGAATACATgtcCATTGGCGACATGACAATGCGGTTTTTT 53 yqjMC26D-F AAAAAACCGCATTGTCATGTCGCCAATGgacATGTATTCTTCTCATGAAAAGGACGGAA 54 yqjMI69T-R CGCTCCAAATGCCTAAGTCTTGGTCAGTcgtTCGTCCTTGAGGGTTAACCGCTGACGCC 55 yqjMI69T-F GGCGTCAGCGGTTAACCCTCAAGGACGAacgACTGACCAAGACTTAGGCATTTGGAGCG 56

To construct pZElac-atoB-mvaS-mvaE (FIG. 2), the atoB was amplified from E. coli genomic DNA with primers atoBAcc-F and atoBPst-R, mvaS was amplified from Enterococcus faecalis genomic DNA with primers mvaSPst-F and mvaSBam-R, and mvaE was amplified from Enterococcus faecalis genomic DNA with primers mvaEBam-F and mvaEXba-R. The vector fragment of pZE was amplified from plasmid pIVC3 (Xiong et al., 2012, Scientific reports 2:311) with primers VecAcc-R and VecXba-F. Then the amplified fragments of atoB, mvaS, mvaE and pZE were digested with Acc65I/PstI, PstI/BamHI, BamHI/XbaI, and Acc65I/XbaI, respectively. These digested fragments were ligated with T4 DNA ligase to form plasmid pZElac-atoB-mvaS-mvaE.

To build plasmids with combinations of different mvaS and mvaE, mvaS genes from S. aureus, L. casei, M. maripaludis and M. voltae were amplified from their corresponding genomic DNA with primer pairs SA.mvaSPst-F/SA.mvaSBam-R, LC.mvaSPst-F/LC.mvaSBam-R, Mm.mvaSPst-F/Mm.remPst-R and Mm.remPst-F/Mm.mvaSBam-R, Mv.mvaSPst-F/Mv.remPst-R and Mv.remPst-F/Mv.mvaSBam-R, respectively. Then mvaS in plasmid pMEV-1 was replaced to form plasmids pZElac-atoB-Sa.mvaS-mvaE, pZElac-atoB-Lc.mvaS-mvaE, pZElac-atoB-Bt.mvaS-mvaE, pZElac-atoB-Mm.mvaS-mvaE and pZElac-atoB-Mv.mvaS-mvaE.

Since the transformed E. coli strain with plasmid pZElac-atoB-Lc.mvaS-mvaE produced the highest level of MEV, more plasmids were constructed with different mvaE based on pMEV-3. mvaE genes from S. aureus, L. casei, M. maripaludis and M. voltae were amplified from their corresponding genomic DNA with primer pairs Sa.mvaEBam-F/Sa.mvaEXba-R, Lc.mvaEBam-F/Lc.mvaEXba-R, Mm.mvaEBam-F/Mm.mvaEXba-R, and Mv.mvaEBam-F/Mv.mvaEXba-R, respectively. Then mvaE in plasmid pZElac-atoB-Lc.mvaS-mvaE was replaced to form pZElac-atoB-Lc.mvaS-Sa.mvaE, pZElac-atoB-Lc.mvaS-Lc.mvaE, pZElac-atoB-Lc.mvaS-Mm.mvaE and pZElac-atoB-Lc.mvaS-Mv.mvaE.

To build plasmid pZAlac-sidI-sidH-ter, sidI and sidH from Aspergillus fumigatus were codon-optimized and synthesized by Integrated DNA Technologies, Inc. (Coralville, Iowa). Then, sidI and sidH digested with Acc65I-HindIII, and HindIII-NheI, respectively, were inserted into the corresponding sites in plasmid pIVC1 (Xiong et al., 2012, Scientific reports 2:311) to from pZAlac-sidI-sidH. The gene ter was PCR amplified by primer pair terNhe-F/terBam-R using T. denticola genomic DNA (Shen et al., 2011, Appl Environ Microbiol 77:2905-2915) as the template. The ter fragment was inserted into the corresponding sites of plasmid pZAlac-sidI-sidH to form pZAlac-sidI-sidH-ter.

To build a plasmid for synthesizing anhydromevalonolactone, sidI and sidH from Aspergillus fumigatus, Neurospora crassa, Phaeosphaeria nodorum, and Sclerotinia sclerotiorum (Grundlinger et al., 2013, Mol Microbiol 88:862-875) were codon-optimized and synthesized by GenScript USA, Inc. (Tulsa, Okla.). Then, sidI and sidH, digested with Acc65I-HindIII and HindIII-NheI, respectively, were inserted into the corresponding sites in plasmid pIVC1 (Xiong et al., 2012, Scientific reports 2:311) to form pZAlac-afsidI-afsidH, pZAlac-ncsidI-ncsidH, pZAlac-pnsidI-pnsidH and pZAlac-sssidI-sssidH, respectively.

To build pZAlac-sidI-sidH-OYE2, sidH was PCR amplified with primers SidHind-F and SidHsal-R using plasmid pZAlac-sidI-sidH as a template. OYE2 was PCR amplified with primers OYE2sal-F and OYE2-Vec using S. cerevisiae genomic DNA as template. The amplified sidH was digested with HindIII and SalI; OYE2 was digested with SalI and NheI, then used to replace sidH in the plasmid pZAlac-afsidI-afsidH to form pZAlac-afsidI-afsidH-OYE2. To build additional variant plasmids, OYE3 was PCR amplified with primers OYE3sal-F and OYE3-Vec using genomic DNA of S. cerevisiae as a template. YqjM was PCR amplified with primers yqjM-F and yqjM-Vec using genomic DNA of B. subtilis as template. The amplified OYE3 was used to replace OYE2 of pZAlac-sidI-sidH-OYE2 to generate pZAlac-sidI-sidH-OYE3. The amplified YqjM was used to replace OYE2 of pZAlac-sidI-sidH-OYE2 to generate pZAlac-afsidI-afsidH-YqjM.

To introduce two point mutants inside the YqjM coding region, three fragments were PCR amplified with primer pairs of yqjM-F/yqjMC26D-R, yqjMC26D-F/yqjMI69T-R, and yqjMI69T-F/yqjM-Vec using B. subtilis genomic DNA as template. Another round of PCR was carried out with primers yqjM-F and yqjM-vec using the last three PCR fragments as template. The PCR product was used to replace OYE2 of pZAlac-afsidI-afsidH-OYE2 to generate pZAlac-afsidI-afsidH-YqjM(mt).

Shake Flask Fermentation

To carry out small-scale fermentation, 125 mL conical flasks with 0.5 g CaCO₃ was autoclaved and dried. Then the flasks were filled with 5 mL M9 medium supplemented with 5 g/L yeast extract, 40 g/L glucose, and antibiotics. 200 μL of overnight cultures incubated in 2×YT medium were transferred into the flasks and placed in a shaker at a speed of 250 rpm. After adding 0.1 mM isopropyl-β-D-thiogalactoside (IPTG), the fermentation was performed for 48 hours at 30° C.

Fed-Batch Fermentation in Bio-Reactor

Fermentation media for bioreactor cultures contained the following composition, in grams per liter: glucose, 10; K₂HPO₄, 7.5; citric acid monohydrate, 2.0; yeast extract, 0.5; MgSO₄.7H₂O, 2.0; Thiamine hydrochloride, 0.008; D-(+)-biotin, 0.008; nicotinic acid, 0.008; pyridoxine, 0.032; ampicillin, 0.1; concentrated H₂SO₄, 0.8 mL; and 1 mL/L of trace metal solution. Trace metal solution contained, in grams per liter: NaCl, 10; Citric acid, 40; ZnSO₄.7H₂O, 1.0; MnSO₄.H₂O, 30; CuSO₄.5H₂O, 0.1; H₃BO₃, 0.1; Na2MoO4.2H₂O, 0.1; FeSO₄.7H₂O, 1.0; CoCl₂0.6H2O, 1.0. The feeding solution contained, in grams per liter: glucose, 600; K₂HPO₄, 7.4; and 10 mL antifoam.

Cultures of E. coli were performed in 1.3 L Bioflo 115 Fermentor (NBS, Edison, N.J.) using an initial working volume of 0.5 L. The fermentor was inoculated with 10% of overnight pre-culture with 2×YT medium. The culturing condition was set at 34° C., dissolved oxygen level (DO) 30%, and pH 7.0. After OD₆₀₀ reached 6.0, 0.2 mM IPTG was added to produce mevalonate. The pH was controlled at 7.0 by automatic addition of 26% ammonia hydroxide. Air flow rate was maintained at 1 vvm in the whole process. DO was maintained about 20% with respect to air saturation by raising stirrer speed (from 300 to 1200 rpm). The fed-batch rate of glucose was determined according to the glucose consumption rate manually. The fermentation process was stopped two days after IPTG addition. Fermentation culture was sampled periodically to determine cell density and production level.

Chemical Reaction and Extraction

The fermentation broth from the bioreactor was harvested by centrifuge, and then was discolored by activated charcoal. The test tubes were filled with 5 mL fermentation broth and concentrated H₃PO₄ or H₂SO₄, then autoclaved for one hour to make anhydromevalonate, and then the concentrations of mevalonate and anhydromevalonate were measured by HPLC. Immiscible organic solvents were used to extraction anhydromevalonate from the reaction mixture.

Metabolite Analysis and Cell Dry Weight Determination

Fermentation products were analyzed using an Agilent 1260 Infinity HPLC (Agilent Technologies, Inc., Santa Clara, Calif.) equipped with an Aminex HPX 87H column (Bio-Rad Laboratories, Inc., Hercules, Calif.) and a refractive-index detector (Agilent Technologies, Inc., Santa Clara, Calif. The mobile phase was 0.01N H₂SO₄ with a flow rate of 0.6 mL/min. The column temperature and detection temperature were 35° C. and 50° C., respectively. Cell dry weight was determined by filtering 5 mL of culture through a 0.45 μm pre-weighed glass fiber filter. After removal of medium, the filter was washed with 15 mL of distilled de-ionized water, dried in a microwave oven for 20 minutes at 300 W, and then weighed. Cell dry weight was determined in triplicate.

Fermentation Scale-Up from 1 L to 500 L

Fermentation media for bioreactor cultures contained the following composition: 10 g/L glucose, 7.5 g/L K₂HPO₄, 2.0 g/L citric acid monohydrate, 0.5 g/L yeast extract, 2.0 g/L MgSO₄.7H₂O, 0.008 g/L thiamine hydrochloride, 0.008 g/L D-(+)-biotin, 0.008 g/L nicotinic acid, 0.032 g/L pyridoxine, 0.1 g/L ampicillin, 0.8 mL concentrated H₂SO₄, and 1 mL/L of trace metal solution (10 g/L NaCl, 40 g/L citric acid, 1.0 g/L ZnSO₄.7H₂O, 30 g/L MnSO₄.H₂O, 0.1 g/L CuSO₄.5H₂O, 0.1; H₃BO₃, 0.1 g/L Na₂MoO₄.2H₂O, 1.0 g/L FeSO₄.7H₂O, and 1.0 g/L CoCl₂.6H₂O). The feed solution contained: 600 g/L glucose, 7.4 g/L K₂HPO₄, and 10 mL antifoam. The 500 L culture conditions were pH 6.8 and a temperature of 34° C.

A culture of E. coli BW25113 was aseptically transferred into a 250 mL baffled shake flask containing 50 mL of 2×YT seed medium (S0 culture). The culture was incubated for eight hours at 34° C. and 200 rpm, and then 30 mL of the S0 culture was used to inoculate a 6 L baffled shake flask containing two liters sterile 2×YT medium. The culture was incubated at 34° C. and 200 rpm for five hours. After the five-hour incubation, the entire contents of the flask was used to inoculate the 75 L bioreactor (New Brunswick Scientific, Eppendorf, Inc., Enfield Conn.). The culture was transferred from the 75 L bioreactor to a 550 L bioreactor (DCI-Biolafitte, St. Cloud, Minn.) through a steam sterilized transfer line after four hours. At 3.5 hours, the OD₆₀₀ reached 6.80 at which time the culture was induced with IPTG (final concentration of 0.4 mM). The feed was started at this time. The glucose was fed exponentially for 9.25 hours of the run using the equation below.

Feed Rate (L/h)=(CDW*V*μ _(max) êμ _(max) *t)/(Feed Conc.*Cell Yield)

Parameters used: CDW=1 g/L; V=200 L; μ_(max)=0.27; Feed Conc.=600 g/L; Cell Yield=0.45 g/g, and t=EFT.

The glucose levels were monitored by using an off-line monitor (YSI, Inc., Yellow Springs, Ohio). The exponential was changed to 0.35 at 9.75 hours to help control the culture glucose concentration at 5-10 g/L.

At 6.75, 7.75 and 8.75 hours EFT, the agitation was set to 250 rpm, the airflow to 200 slpm and the back pressure to 15 psi to control dissolved oxygen levels. At 9.75 EFT, the feed exponential was increased to 0.29 to keep glucose at the desired level. At 10.25 EFT, the dissolved oxygen control was turned on and set to 15%, initially, and later set to 20% for the remainder of the run. The feed pump was varied at each time point to try and maintain glucose between 5-10 g/L. After observing flat culture growth and slowing glucose consumption, the reactor was cooled and prepared for harvest at 36 hours EFT.

The concentrations of glucose, acetate, mevalonate and biomass are shown in FIG. 10.

Example 2 Bacterial and Growth Conditions

BW25113 (rrnB_(T14) ΔlacZ_(WJ16) hsdR514 ΔaraBAD_(AH33) ΔrhaBAD_(LD78)) was used to produce mevalonate (MEV) and β-methyl-δ-valerolactone (βMδVL). (Datsenko et al., 2000, Proc Natl Acad Sci USA 97:6640-6645) All cloning procedures were carried out in the E. coli strain XL10-gold (Stratagene, Agilent Technologies, Inc., Santa Clara, Calif.). These E. coli strains were grown in test tubes at 37° C. in 2×YT rich medium (16 g/L Bacto-tryptone, 10 g/L yeast extract and 5 g/L NaCl) supplemented with appropriate antibiotics (ampicillin 100 μg/mL and kanamycin 50 μg/mL) unless otherwise specified.

Plasmid Construction

Three plasmids were constructed for the biosynthesis of βMδVL (FIG. 9). The first plasmid, pMEV-1, is responsible for MEV production. The second plasmid, pAML-1, is used to produce anhydromevalonolactone (AML); the third plasmid is used to convert AML into βMδVL. Primers for plasmid construction are those listed above in Table 4.

To construct pMEV-1 (FIG. 9), atoB was amplified from E. coli genomic DNA with primers atoBAcc-F and atoBPst-R, and mvaS and mvaE were amplified from E. faecalis genomic DNA with primers mvaSPst-F and mvaSBam-R, mvaEBam-F and mvaEXba-R. The vector fragment of pZE was amplified from plasmid pIVC3 (Xiong et al., 2012, Scientific reports 2:311) with primers VecAcc-R and VecXba-F. Then the amplified fragments of atoB, mvaS, mvaE and pZE were digested with Acc65I/PstI, PstI/BamHI, BamHI/XbaI, and Acc65I/XbaI, respectively. These digested genes were ligated with T4 DNA ligase to form the plasmid pMEV-1.

To build plasmids with combinations of different mvaS and mvaE, mvaS genes from S. aureus, L. casei, M. maripaludis and M. voltae were amplified from their corresponding genomic DNA with primer pairs SA.mvaSPst-F/SA.mvaSBam-R, LC.mvaSPst-F/LC.mvaSBam-R, Mm.mvaSPst-F/Mm.remPst-R and Mm.remPst-F/Mm.mvaSBam-R, Mv.mvaSPst-F/Mv.remPst-R and Mv.remPst-F/Mv.mvaSBam-R, respectively. Then mvaS in plasmid pMEV-1 was replaced to form plasmids of pMEV-2, pMEV-3, pMEV-4, and pMEV-5, respectively.

Since the transformed E. coli strain with plasmid pMEV-3 produced the highest level of MEV, more plasmids were constructed with different mvaE based on pMEV-3. mvaE genes from S. aureus, L. casei, M. maripaludis and M. voltae were amplified from their corresponding genomic DNA with primer pairs Sa.mvaEBam-F/Sa.mvaEXba-R, Lc.mvaEBam-F/Lc.mvaEXba-R, Mm.mvaEBam-F/Mm.mvaEXba-R, and Mv.mvaEBam-F/Mv.mvaEXba-R, respectively.

Then mvaE in plasmid pMEV-3 was replaced to form pMEV-6, pMEV-7, pMEV-8, and pMEV-9, respectively.

To build plasmids to synthesize anhydromevalonolactone (AML), sidI and sidH from A. fumigatus, N. crassa, P. nodorum, S. sclerotiorum (Grundlinger et al., 2013, Mol Microbiol 88:862-875) were codon-optimized and synthesized by GenScript USA, Inc. (Tulsa, Okla.). Then, sidI and sidH, digested with Acc65I/HindIII and HindIII/NheI, were inserted into the corresponding sites in plasmid pIVC1 (Xiong et al., 2012, Scientific reports 2:311) to form pAML-1, pAML-2, pAML-3 and pAML-4, respectively.

To build pMVL-1, sidH was PCR amplified with primers SidHind-F and SidHsal-R and using plasmid pAML-1 as a template. OYE2 was PCR amplified with primers OYE2sal-F and OYE2-Vec using S. cerevisiae genomic DNA as template. The amplified sidH was digested with HindIII and SalI; OYE2 was digested with SalI and NheI, then used to replace sidH in the plasmid pAML-1 to form pMVL-1.

To build pMVL-2, OYE3 was PCR amplified with primers OYE3sal-F and OYE3-Vec using genomic DNA of S. cerevisiae as a template. The amplified OYE3 was used to replace OYE2 of pMVL-1 to generate pMVL-2.

To build pMVL-3, YqjM was PCR amplified with primers yqjM-F and yqjM-Vec using genomic DNA of B. subtilis as template. The amplified YqjM was used to replace OYE2 of pMVL-1 to generate pMVL-3.

To introduce two point mutants into ygjM, three fragments were PCR amplified with primers yqjM-F/yqjMC26D-R, yqjMC26D-F/yqjMI69T-R and yqjMI69T-F/yqjM-Vec using B. subtilis genomic DNA as the template. Another round PCR was carried out with primers yqjM-F and yqjM-vec by using the last three PCR fragments as templates. The PCR product was inserted into pAML-1 to generate pMVL-4.

Shake Flask Batch Fermentation

To carry out small-scale fermentation, 125-mL conical flasks with 0.5 g CaCO₃ were autoclaved and dried. The flasks were filled with 5 mL M9 medium supplemented with 5 g/L yeast extract, 40 g/L glucose and antibiotics. 200 μL of overnight cultures that had been incubated in 2×YT medium were transferred into the flasks and placed in a shaker at a speed of 250 rpm. After adding 0.1 mM isopropyl-β-D-thiogalactoside (IPTG), the fermentation was performed for 48 hours at 30° C. The fermentation results for mevalonate production, anhydromevalonolactone production, and β-methyl-δ-valerolactone production in shake flasks are provided in Tables 5-7.

TABLE 5 Batch fermentation results for mevalonate production Strain Acetate (g/L)* MEV (g/L)* BW25113 with pMEV-1 0.45 ± 0.28 10.75 ± 0.28 BW25113 with pMEV-2 3.11 ± 0.07  5.05 ± 0.28 BW25113 with pMEV-3 0.20 ± 0.03 12.57 ± 0.15 BW25113 with pMEV-4 6.48 ± 0.49 0 BW25113 with pMEV-5 8.80 ± 1.51 0 BW25113 with pMEV-6 0.13 ± 0.05 13.37 ± 0.54 BW25113 with pMEV-7 0.17 ± 0.01 14.62 ± 0.24 BW25113 with pMEV-8 0.13 ± 0.05 10.90 ± 0.39 BW25113 with pMEV-9 0.18 ± 0.02 11.48 ± 0.28 *n = 3, data are shown as mean ± s.d.

TABLE 6 Batch fermentation results for anhydromevalonolactone production Strain MEV (g/L)* AML (g/L)* BW25113 with pMEV-7 and pAML-1 12.36 ± 1.18 0.73 ± 0.06 BW25113 with pMEV-7 and pAML-2 13.59 ± 0.24 0.54 ± 0.02 *n = 3, data are shown as mean ± s.d.

TABLE 7 Batch fermentation results for βMδVL production Strain MEV (g/L)* AML (g/L)* βMδVL (g/L)* BW25113 with pMEV-7 10.19 ± 0.61  0.34 ± 0.03 0.18 ± 0.03 and pMVL-1 BW25113 with pMEV-7 6.77 ± 0.58 0.48 ± 0.03 0 and pMVL-2 BW25113 with pMEV-7 8.85 ± 0.56 0.55 ± 0.01 0 and pMVL-3 BW25113 with pMEV-7 9.39 ± 0.48 0.31 ± 0.01 0.27 ± 0.02 and pMVL-4 *n = 3, data are shown as mean ± s.d.

Fed-Batch Fermentation in Bioreactor

Fermentation media for bioreactor cultures contained the following composition: 10 g/L glucose, 7.5 g/L K₂HPO₄, 2.0 g/L citric acid monohydrate, 0.5 g/L yeast extract, 2.0 g/L MgSO₄.7H₂O, 0.008 g/L thiamine hydrochloride, 0.008 g/L D-(+)-biotin, 0.008 g/L nicotinic acid, 0.032 g/L pyridoxine, 0.1 g/L ampicillin, 0.8 mL concentrated H₂SO₄, and 1 mL/L of trace metal solution (10 g/L NaCl, 40 g/L citric acid, 1.0 g/L ZnSO₄.7H₂O, 30 g/L MnSO₄.H₂O, 0.1 g/L CuSO₄.5H₂O, 0.1; H₃BO₃, 0.1 g/L Na₂MoO₄.2H₂O, 1.0 g/L FeSO₄.7H₂O, and 1.0 g/L CoCl₂.6H₂O). The feed solution contained: 600 g/L glucose, 7.4 g/L K₂HPO₄, and 10 mL antifoam.

E. coli cultures were grown in 1.3-L BIOFLO 115 Fermentor (New Brunswick Scientific, Eppendorf, Inc., Enfield Conn.) using an initial working volume of 0.5 L. The fermenter was inoculated with 10% of overnight pre-culture with 2×YT medium. The culture conditions were set at 34° C., dissolved oxygen level (DO) 30%, and pH 7.0. After OD₆₀₀ reached 5.2, 0.2 mM IPTG was added to produce mevalonate (MEV). The pH was controlled at 7.0 by automatic addition of 26% ammonium hydroxide. Airflow rate was maintained at 1 vvm throughout the process. Dissolved oxygen was maintained about 20% with respect to air saturation by raising stirring speed (from 300 rpm to 1200 rpm). The fed-batch rate of glucose was determined according to the glucose consumption rate manually. The fermentation process was stopped two days after the IPTG was added. The fermentation culture was sampled periodically to determine cell density and production level. The detailed fermentation results are listed in Table 8.

TABLE 8 Fed-batch fermentation results for the production of mevalonate in 1.3 L bioreactor Time (h) Biomass (g/L) Glucose (g/L) Acetate (g/L) MEV (g/L) 0 1.3 4.6 0.85 0 5.5 6.9 12.9 2.25 1.7 16 30.0 0 1.39 24.5 19 34.0 14.3 0.48 34.4 24.5 37.8 24.8 0.35 40.5 31 29.8 34.2 0.33 50.0 40.5 27.0 27.3 1.09 69.6 43 24.5 12.5 1.50 77.1 48 24.0 0 3.48 88.3

Dehydration and Extraction

The fermentation broth from bioreactor was harvested by centrifugation, then filtered through activated charcoal to remove colored contaminants. To determine the optimal level of catalyst for the dehydration, reaction test tubes were filled with 5 mL fermentation broth and 0-12% concentrated H₂SO₄, then autoclaved for one hour (121° C., 15 psi) to produce anhydromevalonolactone. The concentrations of mevalonate (MEV) and anhydromevalonolactone (AML) were measured by HPLC. Chloroform was used to extract AML from the reaction mixture. The results of dehydration are shown in FIG. 5A and Table 9.

TABLE 9 Dehydration results by using different concentration of H₂SO₄ Conversion Selectivity H₂SO₄ (%) MEV (g/L)* AML (g/L)* (%)* (%)* 0 88.3 0 — — 2 66.9 ± 4.2  2.5 ± 0.7 24.2 ± 4.7 15.5 ± 1.3 4 54.6 ± 1.8 23.5 ± 1.6 38.2 ± 2.0 91.9 ± 1.3 6 10.6 ± 0.1 51.6 ± 1.8 88.0 ± 0.1 87.7 ± 3.1 8  2.7 ± 0.1 55.7 ± 0.7 97.0 ± 0.1 86.0 ± 0.9 10  1.7 ± 0.0 58.2 ± 0.6 98.1 ± 0.0 88.8 ± 0.9 12  1.6 ± 0.0 58.1 ± 2.7 98.2 ± 0.0 88.5 ± 4.2 *n = 3, data are shown as mean ± s.d.

Metabolite Analysis and Cell Dry Weight Determination

Fermentation products were analyzed using an Agilent 1260 Infinity HPLC (Agilent Technologies, Inc., Santa Clara, Calif.) equipped with an Aminex HPX 87H column (Bio-Rad Laboratories, Inc., Hercules, Calif.) and a refractive-index detector (Agilent Technologies, Inc., Santa Clara, Calif. The mobile phase was 0.01N H₂SO₄ with a flow rate of 0.6 mL/min. The column temperature and detection temperature were 35° C. and 50° C., respectively. Cell dry weight was determined by filtering 5 mL of culture through a 0.45 μm pre-weighed glass fiber filter. After removal of medium, the filter was washed with 15 mL of distilled de-ionized water, dried in a microwave oven for 20 minutes at 300 W, and then weighed. Cell dry weight was determined in triplicate.

Hydrogenation

Unreduced palladium on activated carbon (10% w/w; Acros Organics, Thermo Fisher Scientific, Inc., Waltham, Mass.) was dried in situ prior to use. Tetrahydrofuran (THF) (Fisher Chemical, Thermo Fisher Scientific, Inc., Waltham, Mass.) was used as received. In a typical hydrogenation procedure, 10 g of catalyst were added to a 300 mL high-pressure reactor with jacketed temperature control and mechanical stirring. The palladium catalyst was held under vacuum at 80° C. for an hour, then cooled to ambient temperature.

Separately, 50 mL of anhydromevalonate was transferred into a solution delivery vessel and sparged with argon for at least 15 minutes. The solution delivery vessel was attached to the reactor and 50 psig argon was applied to displace the contents into the cooled reactor. The argon was released, and the solution delivery vessel detached, stirring was initiated, and the vessel was charged with H₂ to a pressure of approximately 350 psig. The pressure in the vessel was replenished periodically as the hydrogenation progressed until the pressure remained static within the vessel. The reaction was then allowed to stir under H₂ at room temperature overnight to ensure quantitative conversion.

Following depressurization, the reactor was flushed with argon and the reactor contents diluted with THF to facilitate total transfer. The catalyst was removed from the solution by filtration through a filter flask containing a 0.45 μm HVHP membrane (Millipore Corp., Billerica, Mass.). The THF was removed by rotary evaporation to obtain crude β-methyl-δ-valerolactone in typical yields of approximately 93% (conversion >99% by ¹HNMR).

β-Methyl-δ-Valerolactone Purification

Basic alumina (60-325 mesh, Thermo Fisher Scientific, Inc., Waltham, Mass.) was dried under vacuum at 300° C. for three hours, then cooled under argon. Cyclohexane was passed through a solvent purification system, which included a column of activated alumina and a column of molecular sieves operated under a positive pressure of nitrogen gas. The crude β-methyl-δ-valerolactone was dried over calcium hydride (CaH₂) powder (Sigma-Aldrich, St. Louis, Mo.) for 12 hours then distilled under vacuum (50 mTorr, 30° C.). The distilled product was passed through dry basic alumina using cyclohexane as an eluent. The cyclohexane was removed under vacuum to obtain purified β-methyl-δ-valerolactone.

The complete disclosure of all patents, patent applications, and publications, and electronically available material (including, for instance, nucleotide sequence submissions in, e.g., GenBank and RefSeq, and amino acid sequence submissions in, e.g., SwissProt, PIR, PRF, PDB, and translations from annotated coding regions in GenBank and RefSeq) cited herein are incorporated by reference in their entirety. In the event that any inconsistency exists between the disclosure of the present application and the disclosure(s) of any document incorporated herein by reference, the disclosure of the present application shall govern. The foregoing detailed description and examples have been given for clarity of understanding only. No unnecessary limitations are to be understood therefrom. The invention is not limited to the exact details shown and described, for variations obvious to one skilled in the art will be included within the invention defined by the claims.

Unless otherwise indicated, all numbers expressing quantities of components, molecular weights, and so forth used in the specification and claims are to be understood as being modified in all instances by the term “about.” Accordingly, unless otherwise indicated to the contrary, the numerical parameters set forth in the specification and claims are approximations that may vary depending upon the desired properties sought to be obtained by the present invention. At the very least, and not as an attempt to limit the doctrine of equivalents to the scope of the claims, each numerical parameter should at least be construed in light of the number of reported significant digits and by applying ordinary rounding techniques.

Notwithstanding that the numerical ranges and parameters setting forth the broad scope of the invention are approximations, the numerical values set forth in the specific examples are reported as precisely as possible. All numerical values, however, inherently contain a range necessarily resulting from the standard deviation found in their respective testing measurements.

All headings are for the convenience of the reader and should not be used to limit the meaning of the text that follows the heading, unless so specified.

SEQUENCE LISTING FREE TEXT SEQ ID NO: 1 GGGCCCGGTACCATGAAAAATTGTGTCATCGTCAGTGC SEQ ID NO: 2 GGGCCCCTGCAGTTAATTCAACCGTTCAATCACCATCG SEQ ID NO: 3 GGGCCCCTGCAGAGGAGAAATTAACTATGACAATTGGG ATTGATAAAATTAG SEQ ID NO: 4 GGGCCCGGATCCTTAGTTTCGATAAGAACGAACGGTAT SEQ ID NO: 5 GGGCCCGGATCCAGGAGAAATTAACTATGAAAACAGTA GTTATTATTGATGC SEQ ID NO: 6 GGGCCCTCTAGATTATTGTTTTCTTAAATCATTTAAAA SEQ ID NO: 7 GGGCCCGGTACCTTTCTCCTCTTTAATGAATTCGGTCA GT SEQ ID NO: 8 GGGCCCTCTAGAGGCATCAAATAAAACGAAAGGCTCAG TC SEQ ID NO: 9 GGGCCCCTGCAGAGGAGAAATTAACTATGACAATAGGT ATCGACAAAATAAA SEQ ID NO: 10 GGGCCCGGATCCTTACTCTGGTCTGTGATATTCGCGAA SEQ ID NO: 11 GGGCCCCTGCAGAGGAGAAATTAACTATGAAAATCGGG ATTGATGCAATCGC SEQ ID NO: 12 GGGCCCGGATCCTTACCGCTGCTGATATTGACGTTCTT SEQ ID NO: 13 GGGCCCCTGCAGAGGAGAAATTAACTATGCCGGTCGGT ATTGAGGCCATGAA SEQ ID NO: 14 GGGCCCGGATCCTTATGACCAGACGTACTCGCGGTGGA SEQ ID NO: 15 GGGCCCCTGCAGAGGAGAAATTAACTATGAAAGAAGTA GGTATTGTAGGATA SEQ ID NO: 16 TTAGCACCGATGATGTATGCAGCACCACCAGCAGCAGC AGTGTATTCAAGAGCATCTCC SEQ ID NO: 17 GGAGATGCTCTTGAATACACTGCTGCTGCTGGTGGTGC TGCATACATCATCGGTGCTAA SEQ ID NO: 18 GGGCCCGGATCCTTACATTCTAATTTTTCCTCTGTATT TC SEQ ID NO: 19 GGGCCCCTGCAGAGGAGAAATTAACTATGAACGAAGTG GGTATCGTAGGATA SEQ ID NO: 20 CCTACAAGTCCCATACACATTTGTATACCAGCAGTACC TGCTTTACAAGCAAATTCTAA SEQ ID NO: 21 TTAGAATTTGCTTGTAAAGCAGGTACTGCTGGTATACA AATGTGTATGGGACTTGTAGG SEQ ID NO: 22 GGGCCCGGATCCTTACATTCTAATTTTTTCTCTGTATT SEQ ID NO: 23 GGGCCCGGATCCAGGAGAAATTAACTATGCAAAGTTTA GATAAGAATTTCCG SEQ ID NO: 24 GGGCCCTCTAGATTATTGTTGTCTAATTTCTTGTAAAA SEQ ID NO: 25 GGGCCCGGATCCAGGAGAAATTAACTATGAAATTTTAC GAGTTGTCTCCAGA SEQ ID NO: 26 GGGCCCTCTAGATTAATCCCGATTTTCATCTTTTGATT SEQ ID NO: 27 GGGCCCGGATCCAGGAGAAATTAACTATGGAAAATAAC GTTAATATTGAAGA SEQ ID NO: 28 GGGCCCTCTAGATTATCTTCCAAGTTCAGAATGCGCTT SEQ ID NO: 29 GGGCCCGGATCCAGGAGAAATTAACTATGAACAATATA AAAAATAATAATGA SEQ ID NO: 30 GGGCCCTCTAGATTACCTTCCTAATTCCGAATGTGCTT SEQ ID NO: 31 GGGCCCGGTACCATGGAACACTCGGGTTTCCAGCCGGA SEQ ID NO: 32 GGGCCCAAGCTTTTACCCCTTGTTCATGCGCTCACGCA SEQ ID NO: 33 GGGCCCGGTACCATGGCTGAACTCATCCATTCCACAAT SEQ ID NO: 34 GGGCCCAAGCTTTTATTGACTTGATGATAAGTTGAACA TT SEQ ID NO: 35 GGGCCCGGTACCATGACGATGCAGGCCGAGTCCTCTCC SEQ ID NO: 36 GGGCCCAAGCTTTTAGGCCGTCCTGGATTCGCTGAGTT SEQ ID NO: 37 GGGCCCGGTACCATGGATATCATTGGCGGACAACATCT SEQ ID NO: 38 GGGCCCAAGCTTTTATTTCAGATTCTTTCTAATTATTT SEQ ID NO: 39 GGGCCCGGTACCATGCTTTTTACAAACGATACCCTTGG SEQ ID NO: 40 TGGCTGTACTCTGCAATAAACATGGTTGGCACCCCATA AAGGGCAGTACACTTTTCTTT SEQ ID NO: 41 AAAGAAAAGTGTACTGCCCTTTATGGGGTGCCAACCAT GTTTATTGCAGAGTACAGCCA SEQ ID NO: 42 GGGCCCAAGCTTTTATAATTCTTCCGTTTCTTTTTTCA SEQ ID NO: 43 GGGCCCGCTAGCAGGAGAAATTAACTATGATTATCAAA CCGATGATTCGCAG SEQ ID NO: 44 GGGCCCGGATCCTTAAACAACGTCCATGCGCTCGACAT SEQ ID NO: 45 GGGCCCAAGCTTAGGAGAAATTAACTATGAGCACCGAG GCTCATCCTACTGT SEQ ID NO: 46 GGGCCCGTCGACTTACAACTTGCTCGGGCGCCATTGCG SEQ ID NO: 47 GGGCCCGTCGACAGGAGAAATTAACTATGCCATTTGTT AAGGACTTTAAGCC SEQ ID NO: 48 GAGCCTTTCGTTTTATTTGATGCCTCTAGAGCTAGCTT AATTTTTGTCCCAACCGAGTTT SEQ ID NO: 49 GGGCCCGTCGACAGGAGAAATTAACTATGCCATTTGTA AAAGGTTTTGAGCC SEQ ID NO: 50 GAGCCTTTCGTTTTATTTGATGCCTCTAGAGCTAGCTT AGTTCTTGTTCCAACCTAAATC SEQ ID NO: 51 GGGCCCGTCGACAGGAGAAATTAACTATGGCCAGAAAA TTATTTACACCTAT SEQ ID NO: 52 GAGCCTTTCGTTTTATTTGATGCCTCTAGAGCTAGCTT ACCAGCCTCTTTCGTATTGAAC SEQ ID NO: 53 TTCCGTCCTTTTCATGAGAAGAATACATGTCCATTGGC GACATGACAATGCGGTTTTTT SEQ ID NO: 54 AAAAAACCGCATTGTCATGTCGCCAATGGACATGTATT CTTCTCATGAAAAGGACGGAA SEQ ID NO: 55 CGCTCCAAATGCCTAAGTCTTGGTCAGTCGTTCGTCCT TGAGGGTTAACCGCTGACGCC SEQ ID NO: 56 GGCGTCAGCGGTTAACCCTCAAGGACGAACGACTGACC AAGACTTAGGCATTTGGAGCG SEQ ID NO: 57 GGGCCCAAGCTTAGGAGAAATTAACTATGCCAAGAATC TTCCGTTCTGCCGA SEQ ID NO: 58 GGGCCCGCTAGCTTAGAAGTAATAGCGGCTGATGGTCT SEQ ID NO: 59 GGGCCCAAGCTTAGGAGAAATTAACTATGCGTACCATC GCATCGCTGGAAGA SEQ ID NO: 60 GGGCCCGCTAGCTTACCCGTAGCGGCGCGTGATCGACT SEQ ID NO: 61 GGGCCCAAGCTTAGGAGAAATTAACTATGAGCCAGGTC CAGAACATTCCCTA SEQ ID NO: 62 GGGCCCGCTAGCTTAGCCGATGCTGATCGGCGGCAGTT 

1. A biosynthesized anhydromevalonolactone or anhydromevalonate compound.
 2. A biosynthesized β-methyl-δ-valerolactone compound.
 3. A composition comprising anhydromevalonolactone or anhydromevalonate wherein the anhydromevalonolactone or anhydromevalonate comprises ¹⁴C/¹²C ratio greater than zero.
 4. (canceled)
 5. (canceled)
 6. A composition comprising β-methyl-δ-valerolactone wherein the β-methyl-δ-valerolactone comprises ¹⁴C/¹²C ratio greater than zero.
 7. (canceled)
 8. (canceled)
 9. A recombinant cell modified to exhibit increased biosynthesis of anhydromevalonyl-CoA compared to a wild-type control.
 10. The recombinant cell of claim 9 wherein the cell exhibits an increased ability to accumulate β-methyl-δ-valerolactone in culture compared to a wild-type control. 11-25. (canceled)
 26. The recombinant cell of claim 9 further modified to exhibit increased biosynthesis of 3-methyl-5-hydroxypentanoyl-CoA compared to a wild-type control.
 27. The recombinant cell of claim 26 wherein the cell exhibits increased enoyl-CoA reductase activity compared to a wild-type control.
 28. (canceled)
 29. The recombinant cell of claim 9 further modified to exhibit increased ability to accumulate anhydromevalonolactone compared to a wild-type control.
 30. The recombinant cell of claim 9 further modified to exhibit conversion of anhydromevalonolactone to β-methyl-δ-valerolactone compared to a wild-type control. 31-36. (canceled)
 37. The recombinant cell of claim 9 wherein the cell comprises or is derived from a member of the genus Escherichia, a member of the genus Serratia, a member of the genus Bacillus, a member of the genus Brevibacterium, a member of the genus Corynebacterium, a member of the genus Clostridium, a member of the genus Pseudomonas, a member of the genus Candida, a member of the genus Lactococcus, a member of the family Saccharomycetaceae, or a member of the genus Cyanobacteria.
 38. The recombinant cell of claim 9 wherein the recombinant cell is modified to decrease native mevalonate consumption compared to a wild-type control.
 39. The recombinant cell of claim 9 wherein the recombinant cell is modified to increase acetyl-CoA flux compared to a wild-type control.
 40. The recombinant cell of claim 39 wherein increasing acetyl-CoA flux comprises decreasing TCA cycle activity compared to a wild-type control, increasing pyruvate dehydrogenase activity compared to a wild-type control, or deleting acetyl-CoA consumption enzymes compared to a wild-type control.
 41. The recombinant cell of claim 9 modified to exhibit increased biosynthesis of anhydromevalonolactone or anhydromevalonate compared to a wild-type control when grown in culture medium comprising a carbon source that that comprises at least one of: glucose, glycerol, xylose, arabinose, glucaric acid, galactaric acid, galacturonic acid, alginate, starch, sucrose, or cellulose.
 42. A method comprising: culturing a recombinant cell of claim 27 under conditions effective for the recombinant cell to exhibit increased biosynthesis of β-methyl-δ-valerolactone compared to a wild-type control.
 43. A method comprising: culturing a recombinant cell of claim 9 under conditions effective for the recombinant cell to exhibit increased biosynthesis of anhydromevalonyl-CoA compared to a wild-type control. 44-46. (canceled)
 47. A method of preparing β-methyl-δ-valerolactone from biosynthesized anhydromevalonolactone or biosynthesized anhydromevalonate comprising hydrogenating the biosynthesized anhydromevalonolactone or biosynthesized anhydromevalonate to form β-methyl-δ-valerolactone.
 48. The method of claim 47 wherein the anhydromevalonolactone or anhydromevalonate is hydrogenated in the presence of a heterogeneous catalyst or homogenous catalyst.
 49. The method of claim 48 wherein the heterogeneous catalyst comprises: palladium on activated carbon; nickel on silica; or nickel on alumina.
 50. The method of claim 48 wherein the homogeneous catalyst comprises NaBH₄ or LiAlH₄. 51-55. (canceled)
 56. The method of claim 47 exhibiting a β-methyl-δ-valerolactone recovery of at least 70%. 57-59. (canceled)
 60. A method comprising: culturing a recombinant cell modified to exhibit increased biosynthesis of mevalonate or mevalonolactone compared to a wild-type control under conditions effective for the recombinant cell to produce biosynthesized mevalonate or biosynthesized mevalonolactone; and converting the biosynthesized mevalonate or biosynthesized mevalonolactone to anhydromevalonolactone or anhydromevalonate.
 61. (canceled)
 62. The method of claim 60 wherein converting the mevalonate or mevalonolactone to anhydromevalonolactone or anhydromevalonate comprises dehydrating the mevalonate or mevalonolactone using a dehydration catalyst. 63-78. (canceled) 